Processes for producing lithium compounds using reverse osmosis

ABSTRACT

Provided are methods of extracting lithium from a lithium containing solution, as well as the resulting compositions. The method includes supplying a lithium containing solution to a lithium capture step, the lithium capture step being operable to capture lithium from the lithium salt containing solution. The method further includes recovering lithium from the lithium capture step to produce a lithium rich stream. In especially preferred methods, the lithium capture step is performed to increase the lithium to sodium ratio above at least 1:1. Optionally, the lithium rich stream can be purified to remove divalent ions and borate ions. The lithium rich stream is then concentrated by supplying the lithium rich stream to a reverse osmosis step to produce a concentrated lithium rich stream.

CROSS-REFERENCE TO RELATED APPLICATION

This application claims the benefit of and priority to U.S. Provisional Application No. 62/640,898, filed Mar. 9, 2018, which is hereby incorporated by reference in its entirety for all purposes.

TECHNICAL FIELD

The present disclosure generally relates to the field of recovering lithium from lithium containing solutions. More particularly, the present disclosure relates to the preparation of various lithium compounds, and especially to the preparation of concentrated lithium solutions using reverse osmosis.

BACKGROUND

Brines can include various metal ions, particularly alkali and alkaline earth metals, in varying concentrations, depending upon the source of the brine. Geothermal brines are of particular interest for a variety of reasons. First, geothermal brines can provide a source of energy because hot geothermal pools are stored at high pressure underground. When the hot geothermal pools are released to atmospheric pressure, it can provide a flash-steam. The flash-steam can be used, for example, to run a power plant. Additionally, geothermal brines typically contain various useful metals, such as, lithium, lead, silver, and zinc, each of which can be recovered from the brine for further use.

Smackover brines are also of interest because these brines are used to extract bromine and salts such as, for example, calcium and magnesium chloride. The brines also have significant concentrations of lithium, for example, up to 100 to 400 mg/kg, in certain wells. Because the wells are used for bromine production, useful chemicals can be extracted from a previously “mined” brine. Lithium may also be recovered from ores, as the ore may be baked with sulfuric acid, and the product leached with water.

Typically, the economic recovery of lithium from natural, predominantly chloride, brines (which may vary widely in composition), depends not only on the overall lithium content, but also upon the concentrations of interfering ions, particularly calcium and magnesium, which can greatly affect the performance and economics of lithium recovery. Magnesium can be difficult to remove because it is chemically similar to lithium in solution. Generally, at low concentrations, magnesium may be removed by precipitation with lime as magnesium carbonate. However, at higher magnesium concentrations, removal with lime is not feasible.

Although conventional processing of ores and brines makes it possible to eliminate some portions of interfering ions, there remains a need for the simplified removal of interfering ions from brines for the production of lithium carbonate and other lithium compounds.

SUMMARY

In some embodiments, the present disclosure relates to systems, devices, and methods for isolation and concentration of lithium from various sources. In some embodiments, a lithium containing solution (e.g., from a geothermal brine) is pretreated to reduce or eliminate silica and then further processed to render the solution suitable for concentration by reverse osmosis. In other embodiments, the processing utilizes a lithium-specific sorbent that preferentially binds lithium, and particular loading, recycling, and elution profiles are employed to significantly and specifically enrich lithium ions over other ions (e.g., sodium, calcium, manganese, etc.). The osmotic pressure in the obtained solutions is almost entirely a function of lithium ion concentration, and lithium can be further processed in various manners to lithium hydroxide or lithium carbonate.

In other embodiments, a method of extracting lithium from a lithium containing solution includes: supplying a lithium containing solution to a lithium capture step, the lithium capture step being operable to capture lithium from the lithium salt containing solution; recovering lithium from the lithium capture step to produce a lithium rich stream; optionally purifying the lithium rich stream to remove divalent ions and borate ions; and concentrating the lithium rich stream by supplying the lithium rich stream to a reverse osmosis step to produce a concentrated lithium rich stream.

In yet another embodiment, a method of extracting lithium from a lithium containing solution, includes: supplying a lithium containing solution to a lithium capture step, the lithium capture step being operable to capture lithium from the lithium salt containing solution; recovering lithium from the lithium capture step to produce a lithium rich stream; purifying the lithium rich stream to remove divalent ions and borate ions; concentrating the lithium rich stream by supplying the lithium rich stream to a reverse osmosis step to produce a concentrated lithium rich stream; purifying the concentrated lithium rich stream by removing sodium and potassium ions to produce a concentrated lithium rich stream having reduced sodium and potassium ion concentrations.

In some embodiments, a method of extracting lithium from a lithium containing solution, includes: supplying a lithium and silica containing solution to a silica management process to produce a silica lean lithium containing solution; supplying the silica lean lithium containing solution to a lithium capture step, the lithium capture step being operable to capture lithium from the lithium salt containing solution, and where at least a portion of eluate obtained from a sorbent in the lithium capture step is recycled to the sorbent to increase a ratio of lithium to sodium in a lithium rich stream; recovering lithium from the lithium capture step to produce the lithium rich stream; purifying the lithium rich stream to remove divalent ions and borate ions; concentrating the lithium rich stream by supplying the lithium rich stream to a reverse osmosis step to produce a concentrated lithium rich stream; further concentrating the concentrated lithium rich stream to produce a twice concentrated lithium rich stream; and purifying the twice concentrated lithium rich stream by removing sodium and potassium ions to produce a concentrated lithium rich stream having reduced sodium and potassium ion concentrations.

In some embodiments, a method of extracting lithium from a lithium containing solution, includes: processing a lithium containing solution in a lithium capture step by contacting the lithium containing solution with a sorbent material to capture lithium and produce an eluate of the sorbent; recovering lithium from the eluate in the lithium capture step to produce a lithium rich stream; concentrating the lithium rich stream by processing the lithium rich stream in a reverse osmosis step to produce a concentrated lithium rich stream; recycling at least a portion of the eluate back to the sorbent, wherein the portion of the eluate comprises a fraction from an area of peak lithium concentration. In some aspects, the concentrated lithium rich stream is further concentrated by solvent extraction.

BRIEF DESCRIPTION OF THE DRAWINGS

The patent or application file contains at least one drawing executed in color. Copies of this patent or patent application publication with color drawing(s) will be provided by the Office upon request and payment of the necessary fee.

FIG. 1 is a flow chart of a method for producing lithium hydroxide from a geothermal brine according to one embodiment.

FIG. 2 is a flow chart of a method for producing lithium carbonate from a geothermal brine according to one embodiment.

FIG. 3 is a flow chart of a method for concentrating a stream from a lithium capture step in a process of producing lithium hydroxide according to one embodiment.

FIG. 4 is a flow chart of a method of using reverse osmosis to concentrate a stream from a lithium capture step in a process of producing lithium carbonate according to one embodiment.

FIG. 5 is a schematic diagram of a system for producing lithium carbonate from a geothermal brine according to one embodiment.

FIG. 6 is a schematic diagram of a first embodiment of system for producing lithium carbonate from a geothermal brine according to one embodiment.

FIG. 7 is a schematic diagram of a second embodiment of system for producing lithium carbonate from a geothermal brine according to one embodiment.

FIG. 8 is a schematic diagram of a third embodiment of system for producing lithium carbonate from a geothermal brine according to one embodiment.

FIG. 9 shows an exemplary series of elution profiles for lithium from a sorbent according to one embodiment.

FIG. 10 shows an exemplary series of elution profiles for lithium and other ions from a sorbent during load, wash, and strip cycles.

FIG. 11 shows an exploded view of a portion of FIG. 10.

FIG. 12 shows an exemplary series of elution profiles for lithium and other ions from a sorbent during load, wash, and strip cycles according to one embodiment.

FIG. 13 shows an exploded view of a portion of FIG. 12.

FIG. 14 shows a system for extracting lithium in a column according to one embodiment.

DETAILED DESCRIPTION OF THE INVENTION

Generally, the present disclosure relates to processes for producing lithium hydroxide and lithium carbonate from a lithium salt-containing brine. In some embodiments, the processes include a step that concentrates lithium (Li) via a sorbent that allows for selective lithium retention and recovery, and further steps that concentrate the recovered lithium product via reverse osmosis.

As used herein, the term brine refers to a solution of alkali and/or alkaline earth metal salt(s) in water, wherein the concentration of salts can vary from trace amounts up to the point of saturation. Generally, brines suitable for the methods described herein can be aqueous solutions that may include alkali metal or alkaline earth chlorides, bromides, sulfates, hydroxides, nitrates, and the like, as well as natural brines. Brines can be obtained from natural sources, such as, Chilean brines or Salton Sea geothermal resource brines, geothermal brines, sea water, mineral brines (e.g., lithium chloride or potassium chloride brines), alkali metal salt brines, and industrial brines, for example, industrial brines recovered from ore leaching, mineral dressing, and the like. The present methods are equally applicable to artificially prepared lithium salt solutions.

The method steps disclosed throughout the present disclosure are not provided in any specific order and may be used interchangeably, unless otherwise specified.

Accordingly, in some embodiments, the present methods include the preparation and recovery of lithium carbonate from solutions that include, in addition to lithium, other various monovalent, divalent, and multivalent cations (e.g., potassium (K), sodium (Na), calcium (Ca), barium (Ba), magnesium (Mg), manganese (Mn), etc.), as well as various monovalent, divalent, and multivalent anions (e.g., sulfate, chloride, phosphate, etc.)

In certain embodiments, silica may be present in the lithium salt containing solution or geothermal brine, and may be removed by a variety of known methods (e.g., U.S. Pat. No. 4,016,075), prior to use in the methods described herein. Thus, in certain embodiments, the methods for the preparation of lithium carbonate described herein can include a silica management step.

The following methods and method steps are in no particular order and may not be sequential.

FIG. 1 shows a flow chart of a method for producing lithium hydroxide from a geothermal brine according to one embodiment. The method 100 generally includes processing a lithium salt containing brine, such as for example, a geothermal brine, in the following steps: a silica management step 110, a lithium capture step 120 (lithium salt extraction step), an optional concentration of lithium containing solution step 130, an electrochemical production of lithium hydroxide step 140, an evaporation/crystallization step 150, and a lithium hydroxide isolation and drying step 160. The term “lithium” as used herein refers to ionic forms of lithium and as such will include, for example, lithium salts such as lithium halides, lithium sulfates, and lithium nitrates, or some combination thereof. In some embodiments, the lithium salt is lithium chloride.

FIG. 2 shows a flow chart of a method for producing lithium carbonate from a geothermal brine according to one embodiment. The method 200 for producing lithium carbonate generally includes a step of processing a lithium salt containing brine, such as for example, a geothermal brine, in the following steps: silica management step 210, lithium capture step 220 (lithium salt extraction step), electrochemical production of lithium hydroxide step 240, carbonation of lithium hydroxide step 250, and lithium carbonate isolation step 260. In this method 200, lithium hydroxide is converted to lithium carbonate.

In some embodiments, after lithium capture step 220, the method can optionally include concentration of lithium containing solution step 230. In some versions of method 200, after optional step 230, the lithium containing solution may be reacted with sodium carbonate to produce lithium carbonate.

Referring to FIG. 3, provided is a method 300 for the isolation and concentration of lithium ions from a brine or other lithium containing solution, and the optional subsequent production of lithium carbonate therefrom, according to another embodiment. The brine is supplied to silica management step 310, wherein silica is removed from the brine to produce a silica-free brine or lithium containing solution. After silica management step 310, lithium ions are removed from the silica-free brine or lithium containing solution in lithium capture step 320 to form a lithium ion containing solution. The lithium ion containing solution produced from lithium capture step 320 is concentrated via reverse osmosis step 330 to produce a concentrated lithium ion containing solution. After reverse osmosis step 330, there can be optional further concentration of the lithium containing solution, followed by an optional purification step to remove sodium and potassium before the solution is fed to electrochemical production of lithium hydroxide step 340.

Methods to remove sodium and potassium from lithium chloride solutions are well known and include those described in: U.S. Pat. No. 4,920,588; Nakajima, Yasushi et al, “Sodium Selective Ion-Exchange Properties of Zirconium Phosphate, HZr₂(PO₄)₃, and Its Application for the Removal of Sodium Ions,” Analytical Sciences Vol. 12, December 1996, pp. 935-940; and Sun, Jian-Zhi, “Synthesis and Absorption Properties of Novel Na Specific Sorbent,” Journal of Chilean Chemical Society v.53(4), 2008 pp. 1682-1683. Additionally, gains in purity of lithium hydroxide monohydrate can be made by employing a sorbent to remove potassium and sodium impurities.

Optionally, the concentrated lithium ion containing solution from the reverse osmosis step 330 can then be fed through additional process steps to produce lithium hydroxide. In this optional process, the concentrated lithium ion containing solution from reverse osmosis step 330 is fed to electrochemical production of lithium hydroxide step 340 to produce a lithium hydroxide containing solution. The lithium hydroxide containing solution can optionally be processed in an evaporation/crystallization step 350 to remove water from the lithium hydroxide containing solution to crystallize at least a portion of the lithium hydroxide. In an optional lithium hydroxide isolation and drying step 360, the lithium hydroxide is isolated, recovered, and dried.

Optionally, the lithium ion containing solution from the lithium capture step 320 can also be fed to purification of the lithium ion containing solution step before reverse osmosis step 330, or purification of the lithium ion containing solution could occur after reverse osmosis step 330. This optional purification of the lithium ion containing solution can include removal of divalent ion impurities. Purification of lithium ion containing solution is optional because it will be dependent on the lithium ion concentration from lithium capture step 320. If the lithium ion containing solution from lithium capture step 320 is sufficiently pure for feeding to reverse osmosis step 330, then the optional purification will not be necessary.

Referring to FIG. 4, provided is a method 400 for the isolation of lithium ions from a brine or other lithium containing solution and the subsequent production of lithium carbonate therefrom, according to another embodiment. A brine is supplied to silica management step 410, wherein silica is removed from the brine to produce a silica-free brine or lithium containing solution. The silica-free brine or lithium containing solution is then processed in lithium capture step 420. In lithium capture step 420, lithium ions are removed from the silica-free brine or lithium containing solution to obtain a lithium ion containing solution.

The lithium ion containing solution obtained from the lithium capture step 420 may undergo further optional processing to obtain lithium carbonate. In an optional reverse osmosis step 430, the lithium ion containing solution can be concentrated to produce a concentrated lithium ion containing solution via reverse osmosis. In an optional electrochemical production of lithium hydroxide step 440, the concentrated lithium ion containing solution is supplied to an electrochemical cell to produce lithium hydroxide. Then, the lithium hydroxide can be supplied to carbonation of lithium hydroxide step 450, where lithium hydroxide is converted to lithium carbonate. Finally, in lithium carbonate isolation step 460, lithium carbonate is isolated and recovered.

Referring to FIG. 5, provided is a multistep process for the isolation and concentration of lithium ions from a brine or other lithium containing solution according to one embodiment. A brine is supplied to a silica management step (not shown), wherein silica is removed from the brine to produce a silica-free brine or lithium containing solution 500. The silica-free brine or lithium containing solution 500 is then supplied to lithium capture step 510. In lithium capture step 510, lithium ions are removed from the silica-free brine or lithium containing solution 500 to form a lithium ion containing solution 520. The lithium ion containing solution 520 from lithium capture step 510 is then concentrated in reverse osmosis step 530 to produce a concentrated lithium ion containing solution 540. The reverse osmosis permeate (line 505), which essentially comprises water, is recycled back to lithium extraction as the condensate stream (line 590) produced by the concentration of lithium chloride due to the evaporation of water. Line 600 represents the concentrated lithium chloride stream.

The concentrated lithium ion containing solution 540 can optionally undergo further processing. In an optional electrochemical production of lithium hydroxide step, the concentrated lithium ion containing solution 540 is supplied to an electrochemical cell to produce lithium hydroxide. The lithium hydroxide can be supplied to an optional carbonation of lithium hydroxide step where lithium hydroxide is converted to lithium carbonate. In an optional lithium carbonation isolation step, lithium carbonate is isolated and recovered. The lithium ion containing solution from the lithium capture step can also be fed to an optional purification of lithium ion containing solution step before a reverse osmosis step 530 (not shown), or the purification of lithium ion containing solution step 550 could occur after the reverse osmosis step 530.

This optional purification of lithium ion containing solution step 550 can include removal of divalent ion impurities 580. Purification of lithium ion containing solution is optional because it will be dependent on the lithium ion concentration from the lithium capture step 510. If the lithium ion containing solution 520 from lithium capture step 510 is sufficiently pure for feeding to the reverse osmosis step 530, then the optional purification step 550 will not be necessary. After the optional purification step 550, the purified lithium ion containing solution 560 can undergo optional further concentration of lithium containing solution 570, followed by an optional purification step to remove sodium and potassium before the solution is fed to electrochemical production of lithium hydroxide.

Referring to FIG. 6, in one embodiment of the present method, lithium salt containing solution 610 is provided. As noted above, lithium salt containing solution 610 can be obtained from a variety of sources, including geothermal brines. The lithium salt containing solution is supplied to silica management process 612, which operates to significantly reduce the amount of silica that may be present in lithium salt containing solution 610, such that silicate precipitate 616 and silica-lean lithium salt containing solution 614 are produced. Preferably, after silica management process 612, the silica concentration in silica-lean lithium salt containing solution 614 is less than about 150 ppm, more preferably the concentration is less than about 100 ppm, even more preferably the concentration is less than about 50 ppm, and even more preferably the concentration is less than about 25 ppm. In certain embodiments, the concentration of silica in silica-lean lithium salt containing solution 614 is less than about 20 ppm, less than about 10 ppm, or even less than about 5 ppm. It is understood that silica management process 612 may be omitted or replaced from the process for brines that do not include silica, or brines that have a substantially low initial silica concentration.

In certain embodiments, silica management process 612 can include the step of contacting lithium salt containing solution 610 with activated alumina to remove at least a portion of the silica present. Alumina that includes silica bound thereto can be regenerated by contacting the alumina with sodium hydroxide. Alternatively, the lithium salt containing solution can be contacted with aluminum chloride, which is converted to aluminum hydroxide when brought into contact with the brine, and can be used to precipitate silica present in the lithium salt containing stream. In a further embodiment, iron (II) that may be present in certain lithium containing brines can be oxidized with an oxidant, such as air, hypochlorite, hydrogen peroxide, oxygen, ozone, or a like oxidizing agent, to generate iron (III) chloride, which after adjustment of the pH to above about 5, from an initial pH of about 2.5 to 3.5, will precipitate ferric hydroxide. The ferric hydroxide can adsorb silica from the lithium containing brine. In a preferred embodiment, the pH is adjusted to from about 5 to 6 to induce precipitation of silica and iron. In alternate embodiments, the pH is adjusted to above at least about 4.5 to induce precipitation of silica and iron. In certain embodiments, it is preferred the pH is not increased above about 6, to prevent the precipitation of other ionic species present in the lithium containing brine. In yet another embodiment, iron (II) can be added to the lithium chloride containing solution and oxidized by known means to iron (III), for example, by contacting the iron (II) with an oxidant, such as air, oxygen, ozone, hypochlorite, hydrogen peroxide, or other suitable oxidizing agent. Contacting silica present in the lithium chloride containing solution with the iron (III) compound forms a precipitate when the pH is adjusted to between about 4.5 and 6 with the addition of lime or similar base. In a preferred embodiment, the pH is adjusted to from about 5 to about 6. In alternate embodiments, the pH must be adjusted to above at least about 4.5 for the silica and iron to precipitate. In certain embodiments, it is preferred the pH is not increased above about 6, to prevent the precipitation of other ionic species.

In addition, silica management process 612 can include any known means for removing a portion of the silica present in the feed stream, while at the same time maintaining the initial concentration of lithium. In one embodiment, lithium chloride containing solution 610 can be contacted with aluminum chloride, iron chloride, aluminum hydroxide, or the like, to form a precipitate with the silicon dioxide. Contacting can be facilitated by known means, such as a mixing device. Solid silica precipitate 616 removed from lithium chloride containing solution 610 can be collected and removed from the mixing device (or other device), by known means, such as screening or filtering, to yield lithium chloride containing stream 614 that is substantially free of silica.

Various membranes can be used to selectively remove specific undesired ions from lithium containing solution 614.

Silica-lean lithium chloride containing stream 614, which is substantially free of silica (measured as SiO₂), can be supplied to lithium capture (or lithium extraction) step 618. In certain embodiments, silica-lean lithium chloride containing stream 614 can be supplied to lithium capture process 618 that includes at least one intercalated lithium sorbent column, which can be configured to absorb and isolate lithium chloride from the silica-lean lithium chloride containing solution, while at the same time allowing other ions, such as calcium, magnesium, and/or sodium, or the like, to pass with waste water stream 622, through the use of a selective molecular sieve, membrane, or other like materials. In embodiments that include more than one intercalated lithium sorbent column, the bulk of the lithium can be removed in the first intercalated lithium sorbent column, with any subsequent “polishing” intercalated lithium sorbent columns being used to minimize overall lithium loss during the recovery process.

In certain embodiments, the intercalated lithium sorbent column can be operated as follows. In some embodiments, the lithium alumina intercalate particles have an average diameter of less than 800 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of less than 700 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of less than 600 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of less than 500 μm. Lithium alumina intercalate particles having an average diameter of less than 400 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of less than 300 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of less than 200 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of less than 100 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of between about 100 and 150 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of between about 150 and 200 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of between about 200 and 250 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of between about 250 and 300 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of between about 300 and 350 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of between about 350 and 400 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of between about 400 and 450 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of between about 450 and 500 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of between about 500 and 550 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of between about 550 and 600 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of between about 600 and 650 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of between about 650 and 700 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of between about 700 and 750 μm. In some embodiments, the lithium alumina intercalate particles have an average diameter of between about 750 and 800 μm. In certain embodiments, the lithium alumina intercalate particles have an average diameter of between about 200 and 800 μm. Alternatively, lithium alumina intercalate particles have an average diameter of between about 300 and 500 μm, alternatively between about 400 and 700 μm, alternatively between about 350 and 650 μm.

In some embodiments, the lithium alumina intercalate particles can be added to a column, having a particle size of less than about 400 microns. The column may be jacketed, insulated or may include means to provide heating or cooling to the column. The column may include a method of distributing liquid and support for the extraction media and can include fritted ends having a pore size of between approximately 25 and 50 μm, although other like means, such as supports of glass wool or perforated plates, and fractal fluid distributors, can also be used instead of fritted ends. In some embodiments, the operating temperature of the column can be maintained at a temperature that is greater than room temperature (20° C.), and is preferably maintained at a temperature above about 70° C., more preferably from about 95° C. to about 110° C.

The column is maintained wet and is unloaded before first use by circulating at least about 1 bed volume, preferably about 2 bed volumes, of deionized strip water 20 that includes approximately 1000 ppm lithium chloride (or other lithium salt), at a flow rate of between approximately 1 and 4 bed volumes/hour, preferably between about 1.5 and 2.5 bed volumes/hour. The column is then contacted with approximately one bed volume of saturated sodium chloride solution containing approximately 200 ppm lithium chloride and is then operated.

In some embodiments, during loading of the column (i.e., during the step of capturing desired lithium salt), high ionic strength solution 614 containing lithium chloride (or other lithium salt) is supplied to lithium capture process 618 and the lithium concentration of the effluent at waste water stream 622 is measured to determine the point at which the column becomes saturated with the lithium chloride. During the lithium ion capture step, the lithium concentration at waste water stream 622 remains fairly constant and relatively low, for example, approximately from 0 to 100 ppm. At this point, the lithium capture process 618 reaches or nears the point of saturation with lithium ions, however, the concentration of the lithium in the effluent increases, thus indicating that the column has either little or no capacity for additional lithium ions. Upon reaching this point of saturation, flow of the solution that includes lithium chloride to lithium capture process 618 is stopped, and the column is flushed with between about 1 and 5 bed volumes of deionized water, preferably between about 1 and 2.5 bed volumes, and most preferably between about 1 and 1.5 bed volumes, to produce a lithium chloride-rich stream 624. It is understood that the apparatus can include various valves and control devices for controlling the flow of the lithium containing solution or the strip solution to the column.

In certain embodiments, after loading the column, but before collection of the captured lithium chloride (or other lithium salt), the column may be flushed with about 1 bed volume of a 26% saturated sodium chloride solution that includes about 200 ppm lithium chloride.

After the removal of lithium chloride (or other lithium salt) from the lithium containing feed stream during lithium capture process 618, which in some embodiments isolates lithium chloride, intercalated lithium sorbent columns can be regenerated and the lithium chloride recovered therefrom. Specifically, at least about 0.5 equivalents of strip water 620 may be supplied to column(s) used in lithium capture process 618 to remove absorbed lithium chloride and produce lithium chloride rich solution 624. In certain embodiments, between about 1 to 2 equivalents of strip water 620, or more equivalents, may be used during the regeneration of the columns. In preferred embodiments, the strip water may include lithium ions for the regeneration of the columns. Optionally, low ionic strength liquids, such as alcohols and water/alcohol mixtures can be used to regenerate the columns. In general, the amount of water utilized from the lithium chloride recovery from the column is minimized by recycling the product streams to maximize lithium content, without affecting the capacity of the extracting media. In this context, it is noted that strip solution exiting the column (typically enriched with lithium) is also referred to herein as eluate.

Lithium chloride-rich stream 624 may have a lithium concentration of between about 1% and 6% by weight, preferably greater than about 1% by weight, more preferably greater than about 3% by weight, based on the total weight of the lithium chloride-rich stream 624. In alternate embodiments, lithium chloride-rich stream 624 may have a lithium concentration of greater than about 0.5% by weight. Lithium chloride-rich stream 624 can undergo lithium concentration 626 by various means including evaporation, reverse osmosis, solvent extraction or a combination of these processes to produce a concentrated lithium chloride stream 630 having lithium in the range of 10 wt. % to 42 wt. %, based on the total weight of the concentrated lithium chloride stream 630. In preferred embodiments, concentrated lithium chloride stream 630 has a lithium concentration of at least 20 wt. %, more preferably 30 wt. %, and still more preferable 42 wt. %, based on the total weight concentrated lithium chloride stream 630. In the most cases, the concentration of sodium and potassium in the concentrated lithium chloride stream 630 are less than 1 wt. % of stream 630.

In certain embodiments, lithium chloride-rich stream 624 and/or concentrated lithium chloride stream 630 can optionally undergo a purification or concentration step prior to being provided to electrolytic process 632. Optionally, a purification step can be employed to remove calcium, magnesium, or other divalent ions such as zinc and manganese that may be present in lithium chloride (or other lithium salt)-rich stream 624 and/or concentrated lithium chloride stream 630. Removal of calcium, magnesium, and/or other alkaline earth metals can be achieved by known means, such as, by increasing the pH and treating the solution with ion exchange, preferably using selective chelating ion exchange resins, or by the addition of a base, such as lime, sodium hydroxide, lithium hydroxide, or the like, and or by the addition of lithium carbonate, sodium carbonate, potassium carbonate, ammonium carbonate, or other suitable carbonate, which can precipitate magnesium and iron hydroxide, as well as calcium carbonate. In alternate embodiments, ion exchange means can be employed to facilitate the removal of calcium, magnesium, and/or other alkaline earth metals. Other bases, such as sodium hydroxide and other hydroxides of alkali metals, can also be used. In certain brines, it may be beneficial to remove boron from the product stream at this point process by known means, such as by precipitation, solvent extraction, or ion exchange. Methods for the isolation and purification of lithium chloride (or other lithium salt) from brines, including geothermal brines, are known in the art, for example, as described in U.S. Pat. Nos. 9,012,357, 8,901,032, 8,753,594, 8,637,428, 6,280,693, 4,348,295, and 4,461,714 and U.S. Patent Application Publication Nos. 2014/0239224 and 2018/0056283, each of which is herein incorporated by reference in its entirety. In some embodiments, such as those focused on removal magnesium ions, the removal of divalent ions step should occur with lithium chloride-rich stream 624.

Alternative sorbent materials for lithium extraction can also be combined with reverse osmosis to enhance the performance of lithium recovery. In some embodiments, sorbent materials may include lithium oxides, lithium cobalt oxide, lithium phosphates, lithium iron phosphate, lithium fluorophosphates, lithium vanadium fluorophosphates, lithium manganese cobalt nickel oxides, lithium alumina, activated alumina, boehmite, cobalt nickel oxides, lithium titanate, lithium manganese oxides, or mixtures thereof. The sorbent materials may be provided in various forms (e.g., powder). In some embodiments, matrices based upon the sorbent compositions (e.g., activated alumina lithium intercalate sorbent) can be prepared by mixing the sorbent material with a polymer, plastic, or other organic or inorganic binder material.

This optional purification lithium chloride-rich stream 624 and/or concentrated lithium chloride stream 630 can include removal of sodium and potassium before the concentrated lithium chloride stream 630 is fed to electrochemical cell 632.

In certain embodiments, the process can optionally include one or more filter or separation-purification step(s) prior to the step of supplying concentrated lithium chloride solution 630 or brine to electrochemical cell 632.

Optionally, the process can include steps for increasing the concentration of the lithium chloride stream. Specifically, lithium concentration step 626 can be utilized for the removal of a portion of the water in the lithium chloride stream, for example, by evaporation, thereby producing a more concentrated lithium chloride (or other lithium salt) solution 630. Exemplary concentration methods can include solvent extraction, electrodialysis, steam evaporation, or solar evaporation. In further embodiments, the lithium concentration is by reverse osmosis. In such methods, the reverse osmosis apparatus is fed lithium chloride-rich stream 624. In some embodiments, the lithium chloride-rich stream that is fed to the reverse osmosis apparatus has at least 1% wt. lithium chloride. In some embodiments, the lithium chloride-rich stream that is fed to the reverse osmosis apparatus has at least 2% wt. lithium chloride. In further embodiments, the lithium chloride-rich stream has no greater than 1000 mg/kg sodium chloride. In further embodiments, the lithium chloride-rich stream has no greater than 100 mg/kg calcium equivalents. Calcium equivalents includes divalent cations, such as calcium, manganese, magnesium, strontium, and barium. Sodium equivalents include sodium and potassium. In order to calculate equivalents, the molecular weight of the component was assessed. For instance, in order to calculate the calcium equivalent of manganese, the concentration of manganese was divided by the molecular weight of manganese and then multiplied by the molecular weight of calcium.

In further embodiments, the lithium chloride-rich stream has no greater than 30 mg/kg boron. In further embodiments, the reverse osmosis apparatus is also fed recycle streams from either the strip water stream from a lithium sorbent column, or from the depleted brine.

In further embodiments, the lithium capture process includes the step of supplying the silica-lean lithium chloride to a lithium sorbent material for the capture of lithium until the lithium sorbent material is saturated with lithium to produce a saturated lithium sorbent material. In some embodiments the lithium sorbent material is an intercalated lithium sorbent. In further embodiments, the recovering lithium salt step comprises stripping the saturated lithium sorbent material with water to produce the lithium rich stream. In some embodiments, the saturated lithium sorbent material is stripped with between about 1 to 4 bed volumes of water. In some embodiments, the saturated lithium sorbent material is stripped with between about 1 to 3 bed volumes of water. In some embodiments, the saturated lithium sorbent material is stripped with between about 1 to 2 bed volumes of water. In some embodiments, the water is a purified water. In some embodiments, the water is deionized water. In some embodiments, the water is recycled from downstream process such as the lithium chloride concentration step.

In some embodiments, water 628 removed from the lithium chloride solution can be recovered, for example by evaporation and subsequent condensation, and resupplied to intercalated lithium sorbent column(s) of lithium capture step 618, or can be supplied to any other step in this or an associated process that requires the supply of water. Alternatively, water 628 can be supplied to a geothermal well. In embodiments employing a concentration step, overall concentration of concentrated lithium chloride-rich solution 630 can be increased to greater than 25% lithium chloride by weight, preferably up to about 40% lithium chloride by weight.

Concentrated lithium chloride-rich solution 630 can be supplied to electrochemical cell 632, which includes at least one anode, one cathode and a permeable membrane, for the electrochemical preparation of lithium hydroxide. Electrochemical cells suitable for large scale production are commercially available from companies, such as, Ineos, DeNora, Chlorine Engineers, and Asahi Glass, to name a few. Specifically, chloride ions are oxidized to chlorine (Cl) at the anode and water is reduced to hydroxide ions and hydrogen gas at the cathode. Preferably, concentrated lithium chloride-rich solution 630 is substantially free of other ions, particularly ions that may interfere with the electrochemical reaction. Optionally, a lithium chloride-rich stream can supplied directly to the electrochemical reaction, without being first being subjected to the silica management and lithium ion sequestration steps, provided that the lithium chloride-rich stream is substantially free of non-lithium ions, particularly non-lithium ions that may interfere with the electrochemical reaction, for example silica, calcium, and magnesium. In certain embodiments, the concentration of sodium and/or potassium ions in concentrated lithium chloride-rich solution 630 is less than about 5% by weight, preferably less than about 3% by weight, more preferably still less than 1%. Cations such as calcium, magnesium, and the like, if at all present, preferably have a total concentration of less than about 20 ppb by weight, more preferably less than about 10 ppb by weight, and even more preferably less than about 5 ppb by weight. Higher concentrations of the interfering ions does not necessarily preclude operation of the electrochemical cell, but instead may reduce the overall life of the cell components, particularly the membrane and/or the overall effectiveness of the production of lithium hydroxide solution.

Similar to that which is noted above with respect to the presence of non-lithium interfering cations, electrochemical cell 632 preferably has a total non-chloride anion content of less than about 5% by weight, preferably less than about 3% by weight, and even more preferably less than about 1% by weight.

The cathode of electrochemical cell 632 can be any suitable material, including nickel, catalyzed nickel, stainless steel, coated stainless steel, mild steel, and the like. Other exemplary catalysts can include mixed ruthenium and nickel compounds, platinum and other similar compounds that have low hydrogen over potential. The total area of the cathode can be adjusted based upon reactor size and desired production. The catholyte feed to the electrochemical cell 632 can be any suitable material having sufficient ions to carry a current. While water may be employed, and in certain embodiments, the addition of lithium carbonate or lithium hydroxide to water may be beneficial to the operation of the cell.

The anode of electrochemical cell 632 can be any suitable material, such as titanium mesh coated with ruthenium oxide, titanium mesh coated with platinum, carbon, or the like. Preferably, the anode is a dimensionally stable anode, allowing for reduced power consumption. Dimensionally stable ruthenium-iridium oxide on titanium or similar corrosion resistant metal anodes are particularly well-suited for chlorine environments as the titanium substrate is resistant to corrosion. In some embodiments, the anode is a dimensionally stable anode selected from much coated with ruthenium oxide, platinum, or carbon. The total area of the anode can be adjusted based upon reactor size and desired production. The anolyte of electrochemical cell 632 can be any suitable material, including a lithium chloride solution having a concentration of between of about 1% by weight to saturation, preferably between 5% and 40% by weight, more preferably between about 10% and 35% by weight and most preferably between 15 and 25% by weight.

The materials for construction of electrochemical cell 632 can be any material that is chemically resistant to chlorine, activated chlorine, oxygenated chlorine species, and other dissolved species that may exist in brine solutions on the anolyte side and lithium hydroxide on the cathode side. Exemplary materials for the construction of electrochemical cell 632 include polytetrafluoroethylene (PTFE), polyvinylidene fluoride (PVDF), HALAR (alternating co-polymers of ethylene and chlorotrifluoroethylene (CTFE)), and other fluorinated or partially fluorinated materials.

The membrane of electrochemical cell 632 can be any suitable semi-permeable cation selective membrane that selectively passes cations and inhibits the passage of anions. Such membranes are known in the art. One exemplary membrane is Nafion® (E.I. DuPont de Nemours & Co.®), particularly the Nafion® 300, 400, and 900/9000 series of materials. Other suitable membranes can be supplied by Flemion®, however any suitable membrane material can be used provided the material is chemically resistant to both chlorine and lithium hydroxide. The membrane may be placed between the anolyte being electrolyzed and the catholyte.

During operation of electrochemical cell 632, a current density of between about 500 and 10,000 A/m² can be applied at a voltage of between about 1.5 and 5 volts. In some embodiments, a current density of between about 2000 and 7000 A/m² is applied. In further embodiments, a current density of between about between 2000 and 4000 A/m² is applied.

Electrochemical cell 632 may be operated at a temperature of between about 60° and 100° C., preferably between about 70° and 95° C., and more preferably between about 80° and 90° C. Cell 632 can be operated at atmospheric pressure, or slightly above atmospheric pressure.

Operation of electrochemical cell 632 produces lithium hydroxide in solution, and also evolves chlorine and hydrogen gas by products, which can be removed from the electrochemical cell via lines 634 and 636, respectively.

The current efficiency of electrochemical cell 632 can be described in several ways, for the production of lithium hydroxide it is at least about 60%, preferably at least about 70%, more preferably at least about 80%, more preferably at least about 90%, more preferably at least about 95%, and even more preferably at up to about 99.9%. The electrolysis can be operated continually until the lithium hydroxide content reaches about 17% by weight, at which time the lithium hydroxide solution may be removed and supplied to a carbonation reactor. At lithium hydroxide concentrations greater than about 17% by weight, the lithium hydroxide monohydrate in solution can begin to precipitate. Electrochemical cell 632 can also be operated under conditions designed to produce lower concentration lithium hydroxide solutions and the lower concentration lithium hydroxide solution can be recycled to and from the carbonation reactor. In certain embodiments, electrochemical cell 632 can also include a feed line (not shown) for supplying water, low concentration lithium hydroxide, low concentration lithium carbonate, or combinations thereof to the cell. The preferred range of operating conditions lies between 2 and 1% wt. as lithium hydroxide and most preferably in the range of 3 to 8 wt. %.

After lithium chloride-rich stream 624 and/or concentrated lithium chloride stream 630 is processed in the electrochemical cell 632, lithium hydroxide solution 636 is supplied from electrochemical cell 632 to carbonation reactor/absorber 638 and can be contacted with carbon dioxide gas 644, for example, in an up-flow fashion. Carbonation reactor/absorber 638 can include a series of trays or other like means that are designed to allow lithium hydroxide 636 to be supplied to the top of the reactor and flow in a downward fashion through the reactor, thereby contacting up-flowing carbon dioxide gas 644, which can be introduced near the bottom of carbonation reactor/absorber 638. In alternate embodiments, carbonation reactor/absorber 638 can include various mixing means designed to facilitate the efficient mixing of liquids and gases. Optionally, carbonation reactor/absorber 638 can be a jacketed batch reactor having thermostatic heating. The reaction produces lithium carbonate solids. The concentration of the lithium carbonate slurry is preferably at least about 1.5% by weight lithium carbonate, more preferably at least about 6% by weight lithium carbonate. Carbon dioxide can be captured and recycled to carbonation reactor/absorber 638 via line 642.

In certain embodiments, the lithium carbonate can be produced by reaction of lithium chloride with sodium carbonate in water, wherein the mixture is heated, preferably to a temperature of between about 90° C. and 95° C., with stirring. The reaction produces solid lithium carbonate and a sodium chloride solution, wherein the sodium chloride solution can be separated by filtration from the desired lithium carbonate solids.

In certain embodiments, the product of the process is a concentrated solution of lithium chloride, which is produced according to silica management process 612, lithium capture process 618, and lithium concentration 626. It is preferable that the solution produced has a concentration of lithium chloride between 30 wt. % and 42 wt. %, preferably about 36 wt. %. That lithium chloride can be further concentrated to produce crystalline lithium chloride by known evaporation process in the art.

Lithium carbonate containing slurry 640 can be supplied to filter 646, which is operable to separate lithium carbonate containing slurry 640 into water stream 652, which may optionally be resupplied to filter 646, and solid lithium carbonate product 650. Filter 646 can, for example, include a series of screens or filters and water supply 648. Optionally, water can be recycled to the process via line 652. Optionally, lithium carbonate can be concentrated from the lithium carbonate containing slurry 640 by centrifugation or decantation thickening. Water collected during the separation of the solids from the lithium carbonate containing slurry 640 via filter 646 can be supplied to the electrochemical cell 632, or may be recycled to the optional purification steps, or even added back to silica management 612 as a base to increase the pH. In certain embodiments, lithium carbonate solid can be retained on a band or belt filter and supplied to a wash step, wherein hot water, preferably having a temperature of between about 90° C. and 95° C. is used to wash the solids. In certain embodiments, the aqueous solution collected via filter 646 can have a pH of greater than about 9, most likely having a pH between about 10-12. Alternatively, sufficient acid can be added to the aqueous solution to achieve a pH of between about 5 and 8.5, and the acidified water can then be supplied to the intercalated lithium sorbent column(s). Alternatively, the solution can be returned directly to the cathode side of the electrolysis cell without prior neutralization. Still further recycling possibilities include using the strip water in the regeneration of the ion exchange processes to purify the lithium chloride stream.

In some embodiments, the solid lithium carbonate 650 is supplied to a drying station 654, which can optionally include heating means, as well as lines for supplying nitrogen or other inert gases to the drier. Dried lithium carbonate product 656 can then be collected, packaged and transported for further use.

Referring now to FIG. 7, an another embodiment for the production of lithium carbonate is provided. In some embodiments, lithium chloride stream 730 is provided by the process described above and as shown in FIG. 6. In other embodiments, a sodium chloride stream 760 is provided to electrochemical cell 732, which is as described above. Sodium chloride stream 760 is then subjected to electrolysis to produce sodium hydroxide stream 762 and chlorine gas stream 764 and hydrogen gas stream 765. Reaction conditions for the production of sodium hydroxide by electrolysis of sodium chloride are known in the art.

In certain embodiments, the efficiency of the electrolysis of sodium chloride to produce sodium hydroxide is at least about 70%, alternatively at least about 80%, alternatively at least about 90%, or alternatively at least about 95%. In certain embodiments, sodium hydroxide solution 762 is produced in at a concentration of at least about 10% by weight, more preferably at least about 30% by weight, and most preferably about 32 to 35% by weight.

Chlorine gas stream 764 and hydrogen gas stream 765 from electrochemical cell 732 can be combusted and scrubbed with water to generate hydrochloric acid, which may be used within the process, or alternately may be purified, compressed, and sold commercially.

Sodium hydroxide stream 762 is supplied to carbonation reactor/absorber 738, wherein the sodium hydroxide stream 762 is contacted with carbon dioxide steam 744, for example, in an up-flow fashion. Carbonation reactor/absorber 738 can include a series of trays, designed to allow sodium hydroxide stream 762 to be supplied to the top of the reactor and flow in a downward fashion through the reactor, thereby contacting up flowing carbon dioxide gas 744, which can be introduced near the bottom of the reactor, to produce sodium carbonate solution or slurry 766. In alternate embodiments, carbonation reactor/absorber 738 can include various mixing means designed to facilitate mixing of liquids and gases. The concentration of the solution is preferably at least 15% by weight sodium carbonate, more preferably at least 25% by weight sodium carbonate. Carbon dioxide can be captured and recycled to carbonation reactor/absorber 738 via line 742.

Sodium carbonate solution or slurry 766 is supplied to reactor 768 wherein the solution is contacted with lithium chloride solution 730 to produce slurry 770, which includes lithium carbonate and sodium chloride solution. The step of contacting sodium carbonate solution 766 and lithium chloride solution 730 in the reaction vessel can be at a temperature greater than about 60° C., preferably greater than about 80° C., and even more preferably between about 90° C. and 95° C. In certain embodiments, reaction vessel 768 can be a stirred tank reactor. Alternatively, reaction vessel 768 can be a standard crystallizer. In some embodiments, lithium carbonate is present as a precipitate, while sodium chloride remains in aqueous solution.

Slurry 770, which includes solid lithium carbonate and aqueous sodium chloride, is supplied to separator 772, which can include various means for the separation of solids from liquids including, for example, centrifuge, settling tank, filters, screens, and the like, to produce lithium carbonate product stream 774 and sodium chloride brine solution 776. In order to attain improved product quality, the lithium carbonate can be treated to remove sodium, potassium, and/or chloride ions trapped in the interstitial space of the lithium carbonate precipitate, such as by washing with water, preferably hot water, or by like means. In certain embodiments, separator 772 can be a band filter or rotary drum, and can optionally be fed through a counter current wash system for the removal of residual sodium chloride. Separator 772 can also include water inlet 778 to provide water for the washing of the separated solid lithium carbonate. Separator 772 can also include means for drying and/or the removal of water from the solid lithium carbonate, including for example, centrifuge, heaters, blowers, presses, and the like. Separator 772 can include a vacuum filter for removal of water. In certain embodiments, it is desirable to optimize the washing step to both maximize purity of the lithium carbonate while minimizing the amount of water used for washing. Sodium chloride solution 776 can be recycled to electrochemical cell 732 for electrolysis. Lithium carbonate product 774 can have a moisture content of less than about 5% by weight, preferably less than about 2% by weight, and even more preferably less than about 0.5% by weight.

The brine solution 776 from separator 772 can include sodium chloride and lithium carbonate. Generally, depending upon the amount of water utilized in the process and during the wash process, the ratio of sodium chloride to lithium carbonate is at least about 20:1, more preferably at least about 25:1, and even more preferably at least 30:1. In certain embodiments, the ratio of sodium chloride to lithium carbonate in the brine solution can be about 35:1.

In certain embodiments, brine solution 776 can be acidified with hydrochloric acid (not shown) to a pH of less than about 4, preferably about 3, and recycled to electrochemical cell 732. The hydrochloric acid can be supplied from electrochemical cell 732. Such lithium carbonate production method is advantageous because the process eliminates, or nearly eliminates, the production of waste products. Specifically, in certain embodiments, the recycle of unused metal salts, for example sodium chloride, and carbon dioxide, the overall yield can be quantitative or nearly quantitative. Brine solution 776, if required, can be subjected to purification to achieve the desired specifications for sodium chloride anolyte feed to the electrochemical cell 732. As with the process described in detail above in FIG. 6, in certain embodiments, lithium chloride-rich stream 724 and/or concentrated lithium chloride stream 30 can optionally undergo a purification or concentration step prior to being provided to electrochemical cell 732.

Referring now to FIG. 8, another alternate embodiment for the production of lithium carbonate is provided. The method is a single step process wherein sodium carbonate is produced and reacted with recovered lithium chloride, however may require additional input and produces a waste lithium chloride stream that may include small amounts of lithium carbonate entrained therein.

A lithium chloride stream is provided as described above. In some embodiments, sodium chloride stream 860 is provided to electrochemical cell 832. Sodium chloride stream 860 is subjected to electrolysis to produce sodium hydroxide stream 862, chlorine gas stream 864, and hydrogen gas stream 865, respectively.

Sodium hydroxide stream 862 is supplied to mixer 880, wherein the sodium hydroxide stream is combined and mixed with lithium chloride stream 830. Mixing of sodium hydroxide stream 862 and lithium chloride stream 830 can be done by known means, such as by agitators or mixers, with ultrasonic waves, or by the like. Mixer 880 produces mixed stream 882, which includes sodium hydroxide and lithium chloride in aqueous solution. In certain embodiments, it may be preferred that lithium chloride stream 830 has a concentration of lithium chloride of at least about 20% by weight, more preferably at least about 28% by weight, and even more preferably about 42% by weight. Similarly, in certain embodiments, it may be preferred that sodium hydroxide stream 862 has a concentration of sodium hydroxide of at least about 15% by weight, more preferably at least about 25% by weight, and even more preferably about 35% by weight.

Mixed stream 882 is then supplied to carbonation reactor/absorber 884, which can include a series of trays, designed to allow the mixed stream, which includes lithium chloride and sodium hydroxide, to be supplied to the top of the reactor and flow in a downward fashion through the reactor, thereby allowing the mixed stream to sufficiently contact up-flowing carbon dioxide gas 844, which can be introduced near the bottom of the reactor, to produce a lithium carbonate slurry 890. Preferably, carbonation reactor/absorber 884 is maintained at a temperature of between about 90° C. and 100° C. In alternate embodiments, carbonation reactor/absorber 884 can include various mixing means designed to facilitate mixing of liquids and gases. The concentration of the lithium carbonate, e.g., in stream 890, is preferably at least 4% by weight, more preferably at least 8% by weight lithium carbonate. Carbon dioxide can be recycled to carbonation reactor/absorber 884 via line 842.

Lithium carbonate solution 890 is supplied to separator 892 wherein solid lithium carbonate is predicated out via line 894. A solution that includes sodium chloride and possibly a small amount of lithium carbonate is produced as stream 896. Sodium carbonate solution 890, which includes solid lithium carbonate and aqueous sodium chloride, is supplied to separator means 892, which can include various means for the separation of solids from liquids including, for example, centrifuge, settling tank, filters, screens, and the like. Separator means 892 can also include water inlets and outlets (not shown) for the washing of the separated solid lithium carbonate. Separator 892 can also include means for drying and/or the removal of water from the solid lithium carbonate, including for example, centrifuge, heaters, blowers, presses, and the like. A solid sodium carbonate product is collected via line 894. Optionally, a portion of sodium chloride stream 896 can be recycled to electrochemical cell 832. Optionally, the sodium chloride solution can be recycled to the washing step of the lithium extraction media. In certain embodiments, the sodium chloride required for the process can be generated by the selective crystallization of sodium chloride from the geothermal, Smackover, or other brine.

In certain embodiments, contemplated processes may include means for the neutralization of any lithium carbonate that is included in the sodium chloride solution, such as by neutralizing the solution by adding an effective amount of hydrochloric acid or like acid. In embodiments wherein the lithium carbonate can be effectively removed, the solution can be recycled to the electrochemical cell, however, any lithium carbonate included therein may cause problems with the performance of the electrochemical cell.

In further embodiments for an exemplary reverse osmosis system, the lithium containing solution from the lithium capture process is fed to a reverse osmosis system using a pump. From reverse osmosis system, water is fed to the permeate. The concentrated lithium containing stream is fed to the concentrate. The permeate can then be fed back to the reverse osmosis system using the pump. Additionally, the concentrated lithium containing stream can be fed back through the lithium capture process, and to further processing using the reverse osmosis system. Where the reverse osmosis system involves a cascade system, the lithium containing solution from the lithium capture process is fed to a first reverse osmosis system using a first pump. From first reverse osmosis system, first water stream is fed to the permeate and first concentrated lithium containing stream is fed to a second reverse osmosis system using a second pump. From the second reverse osmosis system, the second water stream is fed to permeate and the second concentrated lithium containing stream is fed to third osmosis system using a third pump. From the third reverse osmosis system, the third water stream is fed to permeate and the third concentrated lithium containing stream is fed to the concentrate. Various embodiments of the present invention can include any number of reverse osmosis systems in cascade function. In some embodiments, there are three reverse osmosis systems in cascade. In some embodiments, there are four reverse osmosis systems in cascade. In some embodiments, there are five reverse osmosis systems in cascade. In some embodiments, there are six reverse osmosis systems in cascade. In some embodiments, there are seven reverse osmosis systems in cascade. In some embodiments, there are eight reverse osmosis systems in cascade. In some embodiments, there are nine reverse osmosis systems in cascade. In some embodiments, there are ten reverse osmosis systems in cascade.

A person of ordinary skill in the art will understand how to select appropriate reverse osmosis membranes to use in the present invention. Reverse osmosis membranes can include those supplied by Dow Chemical (Filmtec), Hydranautics, Osmonics (Desal) and Toray. Suitable reverse osmosis membranes include those that are typically spiral wound. Suitable reverse osmosis membranes are also described in Table 1. The list provided in Table 1 is provided by way of example and is not intended to limit the reverse osmosis membranes used in embodiments of the present invention. Potential suppliers along with membrane descriptions are given in Table 1 below. Less preferred membranes are made of cellulose triacetate due to low flux.

TABLE 1 Membrane manufacturer, type and maximum pressure rating. TYPE Membranes Material Max pressure Salt Rejection (NaCl) FILMTEC SW30-2540 Polyamide Thin- 68.9 bar 99.4% SW30-4021 Film Composite 68.9 bar 99.4% SW30-4040 68.9 bar 99.4% SW30HRLE- 82.7 bar 99.75% 4040 SW30HR-380 68.9 bar 99.70% SW30-380 68.9 bar 99.40% Extra low energy SW30XLE-400i 82.7 bar 99.70% SW30HRLE- 82.7 bar 99.75% 400i ultra low energy SW30ULE-400i 82.7 bar 99.70% Boron removal SW30XHR-400i 82.7 bar 99.75% GE-Osmonics AD 2540 FF 68.9 bar DE SAL AD 4040 FF 82.7 bar 99.6% AD 8040F 82.7 bar 99.6% TORAY TM810 Cross-linked 68.9 bar 99.75% TM820-370 Fully aromatic 68.9 bar 99.75% TM820-400 polyamide 68.9 bar 99.75% TM810L 68.9 bar 99.70% TM820L-370 68.9 bar 99.70% TM820L-400 68.9 bar 99.70% TM820H-370 82.7 bar 99.75% Nitto Denko SU810 Cross-linked 68.9 bar 99.75% SU820 Fully aromatic 68.9 bar 99.75% SU820-FA polyamide 68.9 bar 99.75% SU820L 68.9 bar 99.75% SU-820 BCM 98 bar   99.7% HYDRANAUTICS SWC1-4040 Composite 68.9 bar 99.5% SWC3 + Polyamide 82.7 bar 99.8% SWC4 + 82.7 bar 99.8% SWC5-LD 82.7 bar 99.8%

In further embodiments, the lithium capture process is optimized by a series of recycle steps associated with the lithium capture process. For instance, a portion of the strip can be recycled. Additionally, a portion of the load can be recycled. The intention of the recycling is to improve the product lithium chloride purity and maximize its concentration prior to purification or concentration steps.

EXAMPLES Example 1: Carbonation of Sodium Hydroxide

Carbonation of sodium hydroxide was carried out using a 3 liter jacketed reactor with a heating system (manufactured by Syrris Reactor Systems, UK). The reaction was carried out at a temperature of about 95° C. using a one liter of a 9.5 M solution of sodium hydroxide (27.5% solids). Carbon dioxide was supplied for about 1 hour at the rate of 3 L/min. (totaling approximately 8 moles, approximately 1.7 molar equivalents) to ensure the complete conversion of sodium hydroxide. At the end of the carbonation of the sodium hydroxide solution, a clear solution of sodium carbonate was obtained, at which point the carbonation reaction was stopped and heating of the sodium carbonate solution was continued for few minutes. To the clear solution, lithium carbonate seeds were added before reacting it with a lithium chloride solution (404 g lithium chloride in 1000 mL). Experimental yield was 95%. Yields varied for other similar reactions depending upon experimental conditions and were as high as about 100% in some cases. The purity of the isolated lithium carbonate was approximately 96.6% before washing.

Before the first washing of the product stream, the lithium carbonate had the following impurities: Na (71 mg/kg), Ca (2.8 mg/kg), Mg (2.1 mg/kg), Fe (0.3 mg/kg), Ba (0.1 mg/kg), Mn (0.08 mg/kg), and Sr (0.03 mg/kg), for a purity of about 78.4%. After washing with approximately 2-3 volume equivalents of water, the sodium concentration is reduced to undetectable levels and the lithium carbonate had the following impurities: Mg (5.9 mg/kg), Ca (2.9 mg/kg), Ba (0.4 mg/kg), Fe (0.4 mg/kg), Mn (0.07 mg/kg), and Sr (0.07 mg/kg), for a purity of greater than 99%. The washing conditions may affect the amount of sodium carbonate/chloride entrained in the lithium carbonate product.

Example 2: Electrochemical Cell Efficiency

The electrolysis process converts a purified, concentrated lithium chloride solution into a concentrated lithium hydroxide solution for subsequent conversion to lithium bicarbonate. The limiting factor determining the efficiency of the electrochemical cell is the concentration of lithium hydroxide in the catholyte, due to back-migration of hydroxide across the membrane. Therefore, the experiment was designed wherein the electrochemical cell was operated at four different hydroxide concentrations to map the effect of the lithium hydroxide concentration and determine the maximum concentration that could be prepared. The experiment was designed to measure the current efficiency and energy utilization of the dialysis process as a function of hydroxide concentration. Within the electrochemical cell, under an applied field, lithium cations migrate from the anolyte to catholyte, while water present is electrolyzed to H₂ and OH⁻ at the cathode. In theory, each electron passed in the external circuit corresponds to an increase of one lithium hydroxide molecule in the catholyte, leading to an increase in concentration of lithium hydroxide with time. The main inefficiency in the process, the back migration of OH⁻ ions from catholyte to anolyte, is dependent on the OH⁻ concentration of the catholyte. Therefore, the experiments reported here were performed with the intention of maintaining the OH⁻ concentration of the catholyte constant by adding water at a known rate. The efficiency of the reaction was measured by comparing the actual rate of addition of water with the theoretical addition.

Example 3. Electrolytic Production of Lithium Hydroxide from Lithium Chloride

Experimental Set-Up. The electrolysis system consisted of the electrolysis cell having anolyte and catholyte flow systems. Electrolysis of lithium chloride solutions was carried out using an FM01 electrolyzer (a scale model of the FM21 electrolyzer used commercially in the chlor-alkali industry) manufactured by ICI. The electrolyzer included lantern blade-style electrodes (anode: ruthenium oxide coated titanium; and cathode:nickel), and a Nafion® 982 membrane. The active surface area of each electrode was about 64 cm² (4×16 cm), and the cell gap (distance measured anode to cathode) was between about 12-13 mm. The FM01 electrolyzer was operated with the flow parallel to the 16 cm direction (as compared with a flow direction parallel to the 4 cm dimension, as it is intended to be operated), as this improved the management of chlorine and hydrogen gasses evolved from the electrodes. In addition, although anolyte and catholyte flows are normally fed from opposite sides of the cell, in the present experiment, the anolyte and catholyte were fed from the same side of the electrochemical cell.

The anolyte flow system included a feed tank, pump, degassing tank, chlorine scrubber, and collection tank. A lithium chloride solution having a concentration of about 21% by weight was placed in the anolyte feed tank and heated to about 90° C. The heated solution was pumped into the anode chamber of the cell in a single pass mode at a flow rate of about 20 cm³/min, corresponding to a face velocity of about 0.13 cm/s. Upon exiting the cell, the lithium chloride solution and entrained chlorine gas (produced at the anode) were passed through into a degassing tank, which was equipped with a chlorine scrubber, to remove the chlorine. The lithium chloride solution was then pumped into a collection tank for storage.

The catholyte flow system included a feed tank, pump, and water feed system. Lithium hydroxide was placed in the feed tank and heated to about 95° C. and fed to the cathode chamber of the electrochemical cell in recirculating mode at a flow rate of about 50 mL/min, corresponding to a face velocity of about 0.33 cm/s. Water was added continuously to the system using a peristaltic pump to maintain a constant lithium hydroxide concentration. The rate of addition was monitored by the weight loss of the water tank. Nitrogen was bubbled through the catholyte recirculation tank to minimize the reaction of lithium hydroxide and carbon dioxide from the air.

Table 2 summarizes the experimental conditions used in tests to determine the effect of the concentration of the catholyte.

TABLE 2 Experimental parameters for electrolysis experiments. Parameter Value Current Density 3000 A/m⁻² Electrode Area 64 cm² Anolyte Volume 60 cm³ Catholyte Volume 60 cm³ LiCl Inlet Concentration  21 wt% LiCl Inlet pH 0.5-0.7 Temperature 90° C. Time of Operation 2-3 hours Anolyte (LiCl) Flow Velocity   0.13 cm/s Catholyte (LiOH) Flow Velocity   0.33 cm/s

During operation of the electrochemical cell, samples were collected at the catholyte inlet and outlet and anolyte outlet ports every 30 minutes. Cell voltage was monitored at the cell terminals using a handheld multimeter. The difference between the inlet and outlet catholyte hydroxide concentrations and the cell voltage were used to calculate the efficiency and energy consumption of the cell. The results of the concentration of the catholyte are summarized in Table 3. The cell voltage was maintained at approximately 4.3-4.4 V for all of the experimental runs. It was observed that current efficiency decreases with increasing lithium hydroxide concentration. Without wishing to be bound by any one theory, it is believed this decrease in current efficiency may be due to increased back-migration of hydroxide anions across the membrane from the catholyte to anolyte as the lithium hydroxide concentration increases. This also results in increased energy consumption, because all experiments were performed at the same current density and the cell voltage was essentially constant. The experiments suggest that a preferred concentration of lithium hydroxide in the electrochemical cell may be between about 1-2 molar.

Table 3 summarizes the test results. As shown, lithium hydroxide production efficiency increases as lithium hydroxide concentration decreases, having an efficiency of up to about 80-88% for lithium hydroxide solutions having a concentration of about 1 molar (2.4% by weight). Cell voltage is relatively independent of lithium hydroxide concentration, so the efficiency also drives the energy requirement, which decreases to about 5 kWh/kg lithium hydroxide produced at a concentration of about 1 molar. Lithium hydroxide production rate is greatest with lower initial concentrations of lithium hydroxide.

TABLE 3 Summary of Results. LiOH LiOH Production Energy conc. conc. Cell Water Rate* kWh/ (Start) (Final) Voltage Added Efficiency kg LiOH/ kg Test M M V g/min % m²/hr LiOH 1 2.57 3.28 4.37 0.5 35 0.94 15 2 1.62 1.88 4.45 5 65 1.74 8 3 0.94 0.92 4.28 11 80 2.14 5 4 0.69 0.89 4.33 10 88 2.36 5.3 *Calculated (Production rate = 2.68 kg LiOH/m²/hr × efficiency).

Example 4: Carbonation

Chemical Reactor. Lithium hydroxide was carbonated using a 3 L Syrris automated batch reactor system (Syrris Ltd. 27 Jarman Way, UK), having controls for sensing pH, temperature, reagent addition, and sample extraction. The electrolytic studies detailed above suggest that Electrolysis of lithium chloride could at most generate 1 molar or 2.4 wt % lithium hydroxide solution. Indeed, this concentration has been found to be ideal for conducting carbonation studies without clogging issues under our experimental conditions.

Carbonation Reaction Kinetics. The carbonation reaction kinetics of lithium hydroxide were determined by monitoring pH and metal ion concentration in solution (using Atomic Absorption) as the reaction progressed. Approximately 84 g of lithium hydroxide monohydrate was dissolved in 2000 mL of water to prepare a solution having a concentration of about 1 molar (about 2.4% by weight). The reactor jacket was heated using a 30:70 water-glycol mixture and the temperature of the lithium hydroxide solution was maintained at about 95° C. The solution was stirred at 250 RPM with a mechanical stirrer constantly during the carbonation. The carbonating gas tube was maintained at a depth of at least 6 cm in the caustic solution to begin with and the gas flow rate was continuously monitored using a flow meter (Matheson Tri-Gas, USA). As the carbonation progressed, the pH of the solution increased slightly and the completion of the reaction was determined by sudden drop in the pH of the solution, soon after the carbon dioxide flow to the reactor was stopped. The drop in pH coincides with the formation of lithium bicarbonate, which is unstable at higher temperatures. Therefore, the solution was heating/stirring of the solution was continued to decompose lithium bicarbonate that had formed into lithium carbonate. The decomposition of the lithium bicarbonate results in increased pH which stabilized over time. Lithium ion concentration was monitored during the reaction and showed that excess carbonation of the solution can lead to bicarbonate formation.

During carbonation, a slight molar excess of carbon dioxide was added to the lithium hydroxide solution to account for poor mixing of the carbon dioxide into the lithium hydroxide solution. After completion of the carbonation reaction, the solution was hot filtered because the lithium carbonate solubility in water decreases at increased temperatures. The filtered solids were first dried at about 60° C. for about 18 hours, and were then dried at about 120° C. for about 24 hrs to ensure the conversion of any residual lithium bicarbonate that may present in the solids back to lithium carbonate. The carbonation reaction was repeated several times with a 1 molar lithium hydroxide solution under slightly different experimental conditions, and both with and without lithium carbonate seeds. The results are shown in Table 4. Seeding of lithium hydroxide solution with lithium carbonate crystals improved yields. At higher carbon dioxide flow rates (e.g., at 3 L/min and greater), the yield of the carbonation reaction remained high. As shown in Table 3, carbon dioxide feed was maintained at about 2 L/min, although the total amount of carbon dioxide added varied between about 1.25 and 2.5 moles (i.e., between about 0.625 and 1.25 molar equivalents). Experiment 1 in Table 3 included the addition of nitrogen gas to the carbonation vessel. Experiments 3-5 in Table 3 included the addition of between about 0.6% and 1.2% by weight lithium hydroxide seeds. The results show that increased reaction rate can allow for a reduction in the reactor size, and reduced overall cost associated therewith.

TABLE 4 Carbonation Reaction of a 2.4% by Weight Solution of LiOH^(†) Overall Lithium Carbonation Carbonate Solids Pass Reaction Conditions Yield (%)^(#) Recovered (%) 1 CO₂ (2LPM, 2.5 moles) + 100.0% 57%* N₂ (3.7 LPM) 2 CO₂ (2LPM, 1.9 moles) 93% 73% 3 CO₂ (2LPM, 1.5 moles) + 99% 82% 1.2% Li₂CO₃ seeds 4 CO₂ (2LPM, 1.25 moles) + 93% 78% 0.6% Li₂CO₃ seeds 5 CO₂ (3LPM, 1.3 moles) + 96% 82% 1.2% Li₂CO₃ seeds ^(†)Prepared by mixing 84 g lithium hydroxide (LiOH·H₂O) in 2 L water. ^(#)Overall yield includes the amount of lithium carbonate/bicarbonate dissolved in solution and deposited inside the reactor walls. *excessively carbonated and filtered without converting LiHCO₃ back into Li₂CO₃.

Example 5: Concentration of Lithium Chloride Using Reverse Osmosis

A synthetic lithium chloride containing solution was subjected to reverse osmosis at 72 to 80° F.

Test 1: In the first pass the lithium chloride containing solution (LiCl 16,000 ppm; KCl 500 ppm; NaCl 1000 ppm; Ca 3 ppm; and B 1 ppm) was pumped from the Feed tank through line 1 under a pressure of 600 psi at 72° F. into the reverse osmosis system. The feed pump rate was approximately 4 gpm. The permeate (reverse osmosis purified water) was collected and fed to a permeate tank. The weight of permeate was measured at the end of the each pass through the reverse osmosis unit. The retained solution containing the 99% of the Li, Na, K, Ca, Mn & Cl ions, etc. (concentrate) was collected in a concentrate tank. The weight of the concentrate solution in the concentrate tank was measured at the end of the test, In each pass, the pressure was increased until either the maximum pressure (1200 psig) or the maximum recovery (15%) is achieved.

Test 2: In a second test the concentrate from test 1 was transferred into a feed tank and mixed with any remaining unused feed from the previous test. The second pass was conducted in the same manner except that the temperature was 77° F. and the pressure applied was around 740 psi. Once again the concentrate was collected from the concentrate tank and the permeate was fed to the permeate tank. Tests 3 through 7 were repeated in the same manner as test 2 excepting that the pressure was gradually increased as the feed and concentrate solutions became more concentrated in lithium and other salts (Table 5).

A reverse osmosis experiment was conducted to determine the flux and specific flowrate as a function of feed concentration. An synthetic brine mimicking that of the lithium chloride rich stream from the lithium capture step was supplied to a reverse osmosis process. Samples were taken at the beginning and end of each pass. The concentrate from a pass was the feed for the subsequent Pass. The starting artificial brine for Pass 1 contained LiCl 16,000 ppm; KCl 500 ppm; NaCl 1000 ppm; Ca 3 ppm; B 1 ppm. Flux (F) was measured in gallons/sq ft/day (gfd). Specific flow rate (gfd/psi) is a function of feed concentration. Pump flow rate was 4 gpm. The lithium chloride concentration that can be achieved was measured with a reverse osmosis feed pressure up to 1200 psi at a given temperature, as shown in Table 4. The flux remained constant indicating no fouling or salt passage issues at the given pressures. The data is shown in Table 5.

TABLE 5 Mass basis of feed permeate and concentrate streams. Feed Permeate Concentrate Pass psig F Wt(#) LiCl(#) NaCl(#) Wt(#) LiCl(#) NaCl(#) Wt(#) LiCl(#) NaCl(#) % LiCl 1 660 72 100 1.88 0.14 11 0 0 89 1.85 0.08 2.10% 2 740 77 89 2.03 0.3 12 0 0 77 2.01 0.11 2.60% 3 850 73 77 1.95 0.27 10 0 0 67 1.92 0.1 2.90% 4 907 76 67 1.98 0.27 9 0 0 58 1.96 0.1 3.40% 5 1000 83 58 1.94 0.28 8 0 0 50 1.86 0.11 3.70% 6 1117 88 50 1.92 0.28 6 0 0 43 1.89 0.11 4.40% 7 1200 80 43 1.88 0.27 4 0 0 39 1.96 0.11 5.10% Final total 61.2 0.01 0 38.8 1.96 0.11 5.10%

From this, theoretical reverse osmosis pressures were determined.

Example 6: Further Optimization of Lithium Chloride Capture Step for Feed to Reverse Osmosis

The following experiments were conducted to determine an optimum process for the lithium capture step, and to provide feed for subsequent reverse osmosis process.

A standard lab column measuring 2.6 cm×53 cm was prepared with a sorbent made as described in U.S. Pat. No. 8,901,032. The resulting sorbent was screened to a mean particle size of between about 300 and 500 microns and was then slurried with deionized water and poured into the column and backwashed with saturated salt solution to remove fines. The column was loaded with Li from a geothermal brine.

The geothermal brine was a Hudson Ranch geothermal brine that had been subjected to a silica management process. The silica management process was a continuous process for the management of silica. The silica management system included three stirred reaction vessels provided in series. To the first reaction vessel a geothermal brine was provided at a rate of about 6 gpm. Approximately 30 cfm of air was supplied to each reactor and was dispersed through the geothermal brine. After the addition of the air to the first reaction vessel, the pH dropped to between about 2.3 and 3.5. The brine supplied to each of the three reactors is maintained at a temperature of about 95° C.

The geothermal brine from the first reactor was also supplied to the second reactor. An aqueous calcium hydroxide slurry that included between about 15 and 25% by weight calcium hydroxide was supplied to the second reactor at a rate on a wet basis of about 0.5 lb/min. This raised the pH in the second reactor to between about 4.8 and 6.5. The brine in the second vessel in contact with calcium hydroxide slurry was again contacted with air. The addition of calcium hydroxide slurry initiates the precipitation of iron (III) hydroxide and iron silicate. The brine was then supplied from the second vessel to the third reaction vessel where it was again contacted with air. The air to all vessels was supplied at a constant rate, of about 30 cfm. Each of the three reactors included means for stirring to ensure sufficient mixing of the brine, base and air oxidant. The continuous addition of air and base to the reaction vessel results in the precipitation of the iron and silica at rates up to about 0.5 lb/minute, depending upon the concentration of iron and silica in the geothermal brine.

The geothermal brine, including precipitates of iron (III) hydroxide and iron silicate, was then supplied from the third reaction vessel to a clarifier. Water was added to the clarifier. An aqueous flocculant solution of Magnafloc 351, in a concentration between about 0.005% and 1% by weight, such as about 0.025% by weight, was supplied to the clarifier vessel at a rate of about 0.01 gpm.

From the clarifier were produced two streams. First clarifier product stream included the geothermal brine having a reduced concentration of silica and iron, which was then fed to the lithium capture step. Second clarifier product stream included solid silica-iron waste, as well as some geothermal brine.

FIG. 14 shows one embodiment of a system 1400 for extracting lithium in a column from a sorbent with three regenerant solutions. The system 1400 includes a column 1410, a load tank 1420, a depleted brine tank 1425, a recycle cut tank 1430, a product cut tank 1440, and a strip tank 1460. A load (line 1), e.g., a lithium-containing brine solution, was sent to the column 1410. The lithium was stripped from load (line 1) in the column 1410 by treating the column 140 sequentially with three regenerant solutions, starting with the Recycle Cut (line 2), which was used to displace the lithium-containing brine solution from the column 1410, followed by the Recycle Strip (line 5 and line 6), which was used to begin stripping the column and followed finally by a Strip Solution (line 7) of freshly prepared from DI water with 500 mg/kg Li added to complete the elution of Li from the column 1410. Each cycle includes lithium-containing brine solution (line 1), Recycle Cut (line 2), Recycle Strip (lines 5 and 6), and Strip Solution (line 7). The feeds and flow rates are shown in Table 8. This was repeated through at least 50 cycles.

The Recycle Cut (line 2) from the column 1410 is recycled to the load tank 1420. The Recycle Cut (line 3) as shown in Table 8 is defined as the peak area of the strip, where the lithium is the highest concentration, but also where the impurities such as sodium, potassium, calcium, manganese and boron are at their highest. This is recycled and fed into the column 1410 immediately following the loading step. The depleted brine (line 3) that exits from the column 1410 can be sent to depleted brine tank 1425.

The Product Cut (line 4) from the column 1410 is sent to the product cut tank 1440 for further processing (e.g., reverse osmosis system). The Product Cut (line 4) as shown in Table 8 is the portion of the strip that is retained (e.g., in the product cut tank 1440) for processing by the reverse osmosis system. In some aspects, the Product Cut (line 4) should have an average concentration greater than 1600 mg/kg Li (about 1%) and less than 1000 mg/kg Na and less than 500 mg/kg divalent ions expressed as Ca and B less than 100 mg/kg and preferably less than 50 mg/kg.

The Recycle Strip (line 5) from the column 1410 is sent to the recycle strip tank 1430 and can then be sent as Recycle Strip (line 6) to the column 1410. In some embodiments, the Recycle Strip (line 5) and processed in recycle strip tank 1430 and then sent as a modified Recycle Strip (line 6) to the column 1410. The Recycle Strip (lines 5 and 6) as shown in Table 8 is defined as that portion of the Li strip following the Product Cut (line 4), which has a lithium concentration in the range of 700 to 1500 mg/kg, which is too low to be forwarded to the product cut tank 1440 or reverse osmosis system. This Recycle Strip (lines 5 and 6) is recycled to become the feed to produce the product cut as impurities such as sodium, potassium, calcium, manganese and boron are at their lowest.

A Strip Solution (line 7) can be supplied to the column 1410 from a strip tank 1460. The Strip Solution (line 7) can be added to the load (line 1), the Recycle Strip (line (6), or can be independently fed to the column 1410. The Strip Solution (line 7) may comprise freshly prepared from DI water with 500 mg/kg Li added to complete the elution of Li from the column 1410.

The Load Recycle (not shown in FIG. 14) as shown in Table 8 is defined as that portion of the Li loading and strip curves which contains Li at concentrations from 200 up to about 4000 mg/kg where impurities such as sodium, potassium, calcium manganese and boron are at concentrations from about 30% of their concentrations in the feed brine up to their feed brine concentration, which is recycled back to the feed tank, mixed with the geothermal brine and fed to the column during the subsequent load step.

TABLE 8 Feeds and Flow rates to the lithium capture step. Bed Volume BV Flow Rate Column Column Feed (BV)/Cycle Total (BV/hr) Sample # Exit Load 0.4 0.4 12  1 Recycle Strip (geothermal brine) Load 0.4 0.8 12  2 Load Recycle (geothermal brine) Load 14.2 15 12  3-12 Depleted Brine (geothermal brine) Recycle Cut 0.4 15.4 12 13 Depleted Brine Recycle Strip 0.2 15.6 2 14 Depleted Brine Recycle Strip 0.3 15.9 2 15-16 Load Recycle Recycle Strip 0.2 16.1 2 17 Recycle Cut Strip 0.3 16.4 2 18-20 Recycle Cut Strip 1.0 17.4 2 21-30 Product Cut Strip 0.7 18.1 2 31-37 Recycle Strip

Table 9 shows the concentrations of select components in the geothermal brine before the start of each cycle. This brine was sampled before lithium extraction.

TABLE 9 Geothermal Brine Feed Component concentrations Cycle Li (mg/kg) Na (mg/kg) Ca (mg/kg) B (mg/kg) 52 320 56000 33000 435 53 310 59000 33500 460 54 340 61000 32900 440 55 300 58000 34600 445 56 300 58000 32600 440 57 375 63000 35500 465 58 360 61000 33700 455 59 380 56000 31700 420 60 380 56000 31300 425 61 355 58000 32700 425 62 350 59000 33000 425 63 330 58000 32700 435 *(note: this includes some recycling of the recycle cut).

FIG. 9 shows exemplary lithium loading curves for various cycles. When the lithium concentration is in the range of about 500 to 800 mg/kg it is considered to be the tail fraction. The tail fraction can be recycled to be the feed for the product cut. The product cut is the portion of the strip that is retained for processing by the reverse osmosis system. It has an average concentration of the order of about 1600 mg/kg Li and less than about 1000 mg/kg Na and less than about 500 mg/kg and preferably less than 200 divalent ions expressed as calcium equivalents and boron is less than about 100 mg/kg and preferable less than about 50 mg/kg. The recycle cut is the peak area of the strip, where the lithium is the highest concentration, but also where the impurities such as sodium, potassium, calcium, manganese and boron are at their highest. This is recycled and fed into the column instead of the wash step described in the example above.

Table 10 shows the concentrations in the lithium chloride product cut post lithium extraction for cycles 52 to 63. This product cut is fed directly to a reverse osmosis process, or to a purification process, then to reverse osmosis process.

TABLE 10 Component concentrations. Cycle LiCl LiCl NaCl Ca B number (wt %) (mg/kg) (mg/kg) (mg/kg) (mg/kg) 52 1.5% 15,000 268 174 47 53 1.3% 13,000 334 182 29 54 1.4% 14,000 465 176 31 55 1.2% 12,000 293 127 20 56 1.3% 13,000  77  11 26 57 1.2% 12,000  69  92 16 58 1.4% 14,000 528 188 35 59 1.3% 13,000 703 206 32 60 1.6% 16,000 306 180 44 61 1.4% 14,000 145 131 35 62 1.4% 14,000 144 137 39 63 1.2% 12,000  81 109 28

Example 7: Additional Examples for Optimization of Lithium Chloride Capture Step for Feed to Reverse Osmosis

Conventional/Comparative: A column was loaded with sorbent produced by methods described in U.S. Pat. No. 8,901,032 B1 to a depth of 48 cm the column diameter was 2.64 cm. Lithium was extracted and recovered from the geothermal brine according to the following sequence. The flow rate of geothermal brine, the (load), was 60 ml/min and 5.065 liters of geothermal brine were passed through the column. This was followed by a solution of sodium chloride (wash) 62 mol/min until 0.3 liters of solution was passed and finally a strip solution of water containing 500 mg/kg was passed through the column at a rate of 12 ml/min until 0.9 l of solution had been passed through the column. The input data to the column is shown in Table 11, the output data in Table 12 and FIG. 10 (Li Concentration at the outlet read primary Y axis for Li, Mn, Zn, Ba and Zn, read secondary Y axis to read Na, K and Ca) and FIG. 11.

FIG. 11 illustrates one embodiment in which the area of peak lithium concentration includes the most concentrated lithium solution that is extracted from the sorbent. In some embodiments, however, the area of peak lithium concentration can also include impurities. For example, the area of peak lithium concentration may include a large amount of sodium and potentially other impurities (e.g., calcium and potassium). The area of peak lithium concentration may have the highest concentration of the lithium, but also the impurities such as sodium, potassium, calcium, manganese and boron are at their highest in this area.

In some embodiments, the process may include recycling a cut from the area of peak lithium concentration (also referred herein as “recycle cut”) to remove these impurities to produce a purer lithium solution. The recycle can be taken from the area peak lithium concentration during the stripping process. By employing one or more recycles of the peak lithium concentration solution, the peak lithium concentration can be shifted to a later time in the strip cycle. Therefore, the process can produce a purer concentrated lithium stream (see e.g., FIG. 13 “product cut”) which can be fed to the reverse osmosis unit.

For example, comparing FIG. 11 with FIG. 13, the lithium concentration is significantly higher in FIG. 13 between Bed Volume (BV) 13 and 14, whereas a similar position in FIG. 11 (roughly between BV 19.5 and 20.5) has a lower concertation of lithium and significantly higher concentration of sodium. The high sodium content prevents the use of reverse osmosis on these solutions as reverse osmosis has limits on operating pressures to about 1000 to 2000 psi. The high sodium content results in a higher osmotic pressure which has to be overcome for the reverse osmosis to have any practical utility. Thus, by utilizing one or more recycle cuts of the highly concentrated lithium solution as part of the stripping process (e.g., stripping lithium from the sorbent), the area of peak lithium concertation can be shifted in the strip cycle to produce a purer lithium solution with less impurities which can now be fed to the reverse osmosis unit.

TABLE 11 Flow Flow Rate Rate kg ml Cum. 0.28 hr⁻¹ min⁻¹ Volume 1 B Ba Ca Cu K Li Mg Mn Na Pb Rb S Si Sr Zn Feed 4.32 59.9 5.090 452 38.7 28900 4.8 13400 290 70.9 1030 41100 97.5 235 318 4.38 500 563 Brine Feed 5.10 62.0 0.310 <5.0 <1 <5.0 <0.5 32.3 521 <5.0 <0.5 91100 <2 <10.0 <20.0 <2 <0.5 <1 Wash Feed 0.72 11.9 0.901 <5.0 <1 <5.0 <0.5 <10.0 491 <5.0 <0.5 35.9 <2 <10.0 <20.0 <2 <0.5 <1 Strip

TABLE 12 Flow Rate Cum Time ml Volume min min⁻¹ ml B Ba Ca Cu K Li Mg Mn Na Pb Rb S Si Sr Zn 2.5 46.0  115 9.25 <10 412 <0.5 265 914 <5.0 60.4 3130 <2.0 <10.0 <2.0 <2.0 6.19 6.6 Load 5 60.0  265 6.51 2.69 3780 <0.5 2250 631 <5.0 40.8 7420 <2.0 16.5 30.7 <2.0 55.5 2.77 10 60.0  565 159 27.4 29200 0.769 15600 20.9 38 403 48300 48.2 175 256 <2.0 404 233 20 60.0 1165 424 35.9 35300 3.61 19300 <10.0 65.5 1610 55600 97.3 216 308 <2.0 492 713 30 60.5 1770 443 37.2 36600 5.11 20300 31 67.8 1730 54100 97.3 224 305 <2.0 504 743 40 60.0 2370 447 37.2 36800 4.88 20500 132 66.8 1700 54300 102 227 303 <2.0 506 731 50 60.0 2970 457 39.5 38800 4.75 21600 229 70.7 1790 57600 104 243 318 2.49 536 772 55 60.0 3270 456 39.1 38800 4.95 21800 260 70.1 1800 57800 107 243 318 2.58 536 777 60 60.0 3570 430 36.3 36200 4.21 20200 253 65.1 1700 53700 94.5 225 296 2.44 500 742 65 60.0 3870 444 37.8 37800 4.44 21100 274 67.9 1650 56500 101 231 309 2.66 525 748 70 60.0 4170 425 36.2 36500 4.65 20300 264 65.7 1680 54300 96.9 223 291 2.79 508 729 75 60.0 4470 445 38.1 37400 4.13 20900 259 68 1680 55700 97.7 234 304 2.95 519 710 80 60.0 4770 402 33.4 34200 3.8 19100 248 60.6 1590 50600 89.7 203 269 2.23 473 689 85 62.0 5080 435 34.8 33500 4.86 18500 286 60.9 1550 62600 93.1 212 284 2.82 473 650 89  7.8 5111 253 11.6 10200 3.04 5480 449 19.6 512 73400 31.6 62.2 85.8 2.06 141 160 Wash 93 12.3 5160 195 6.45 5140 2.5 2830 396 10.4 333 85900 18.7 29.8 45 <2.0 71.5 95.5 97 12.1 5209 119 3.16 2200 2.36 1580 371 <5.0 176 84700 9.47 11.6 21.3 <2.0 30.9 47.7 101 12.5 5259 86.5 2.22 1350 1.79 980 396 <5.0 124 96100 6.2 <10.0 <20.0 <2.0 18.9 32.7 105 12.8 5310 68.5 1.83 1060 2.34 838 398 <5.0 104 104000 5.63 <10.0 <20.0 <2.0 15.2 29.2 109 12.6 5360 52.2 1.51 852 1.33 500 2370 5.32 167 64100 2.58 <10.0 <20.0 <2.0 12.1 16.3 Product 113 12.4 5410 36.5 <1.0 348 0.674 107 4550 8.08 258 10300 <2.0 <10.0 <20.0 <2.0 4.56 3.13 Cut 117 12.5 5460 22 <1.0 127 <0.5 62.4 2920 <5.0 205 2920 <2.0 <10.0 <20.0 <2.0 1.9 1.38 121 12.5 5510 15.1 <1.0 115 0.51 78.8 2070 <5.0 173 1710 <2.0 <10.0 <20.0 <2.0 1.76 1.63 125 12.4 5559 11.1 <1.0 72.4 <0.5 49.9 1580 <5.0 143 1140 <2.0 <10.0 <20.0 <2.0 1.13 <1.0 129  5.0 5579 9.1 <1.0 64.5 <0.5 46 1370 <5.0 130 1010 <2.0 <10.0 <20.0 <2.0 0.909 <1.0 133 12.4 5629 7.09 <1.0 57.6 <0.5 40.8 1230 <5.0 111 950 <2.0 <10.0 <20.0 <2.0 0.825 <1.0 137 12.5 5679 6.26 <1.0 51.6 <0.5 39 1070 <5.0 101 849 <2.0 <10.0 <20.0 <2.0 0.676 <1.0 141 12.5 5729 <5.0 <1.0 47.2 <0.5 34.7 968 <5.0 85.4 733 <2.0 <10.0 <20.0 <2.0 0.616 <1.0 Recycle to 145 12.5 5779 <5.0 <1.0 65.5 <0.5 46.8 881 <5.0 72.4 768 <2.0 <10.0 <20.0 <2.0 0.838 <1.0 Strip Feed 149 12.5 5829 <5.0 <1.0 55.7 <0.5 41.7 866 <5.0 62.8 606 <2.0 <10.0 <20.0 <2.0 0.748 <1.0 153 12.5 5879 <5.0 <1.0 49.2 <0.5 34.2 836 <5.0 55 537 <2.0 <10.0 <20.0 <2.0 0.636 <1.0 157 12.3 5928 <5.0 <1.0 47.9 <0.5 33.7 816 <5.0 49.1 485 <2.0 <10.0 <20.0 <2.0 0.628 <1.0 161 12.4 5977 <5.0 <1.0 39.5 0.562 27.1 783 <5.0 41.3 436 <2.0 <10.0 <20.0 <2.0 <0.5 <1.0 6005 <5.0 <1.0 35.7 <0.5 24.8 759 <5.0 39.4 405 <2.0 <10.0 <20.0 <2.0 <0.5 <1.0

Inventive Methods suitable for Combination with Reverse Osmosis: A column was loaded with sorbent produced by methods described in U.S. Pat. No. 8,901,032 B1 to a depth of 19.3 inches the column diameter was 1 inch. Lithium was extracted and recovered from the geothermal brine according to the following sequence. The flow rate of geothermal brine, the (load), was 50 ml/min and 3.058 liters of geothermal brine were passed through the column. Subsequently, recycle cut was fed to the column according to flow diagram in FIG. 5 at the same flow rate for a total of 0.1 liters. Subsequently, recycle strip was fed to the column at 11 ml/min to a total of 0.26 l and finally feed strip solution was fed to the column. The results of the extraction and resulting strip procedure are shown in FIG. 12 (Li Concentration at the outlet read primary Y axis for Li, Mn, Zn, Ba and Zn, read secondary Y axis to read Na, K and Ca) and FIG. 13 along with Table 13.

TABLE 13 Flow Rate/ ml Cumulative BV B Ba Ca Cd Cu Fe K Li min- 

Volume/1 mg/kg Feed Brine 50.1 3.058 11.4 405 32 34700 3 4 <1.0 18400 259 Feed Recycle 50.1 0.100 0.4 229 3 1470 <0.5 <0.5 <1.0 613 2750 Cut Feed Recycle 10.9 0.261 1.0 29 <1.0 84 <0.5 <0.5 <1.0 40 979 Strip Feed Strip 9.2 0.519 1.9 <5.0 <1.0 <5.0 <0.5 <0.5 <1.0 <10.0 519 3.937 14.7 Depleted Brine 1.970 7.3 356 30 33000 3 4 <1.0 17500 16 Lag Brine 1.259 4.7 381 29 31800 3 5 <1.0 16900 144 Recycle Brine 0.155 0.6 164 5 4880 <0.5 1 <1.0 2590 1400 Recycle Cut 0.110 0.4 268 4 1850 <0.5 <0.5 <1.0 841 3000 Product Cut 0.327 1.2 102 <1.0 367 <0.5 <0.5 <1.0 149 1800 Recycle Strip 0.219 0.8 40 <1.0 108 <0.5 <0.5 <1.0 47 1100 Mg Mn Na Pb Rb S Si Sr Zn mg/kg Feed Brine 63 1690 57600 82 215 263 3 481 656 Feed Recycle 9 640 1870 <2.0 <10.0 <20.0 <2.0 22 6 Cut Feed Recycle <5.0 85 114 <2.0 <10.0 <20.0 <2.0 1 <1.0 Strip Feed Strip <5.0 <0.5 <10.0 <2.0 <10.0 <20.0 <2.0 <0.5 <1.0 Depleted Brine 58 1530 53100 82 204 245 <2.0 457 648 Lag Brine 59 1580 53400 78 198 237 <2.0 444 603 Recycle Brine 15 551 7420 7 20 35 <2.0 74 54 Recycle Cut 12 721 2360 <2.0 <10.0 <20.0 <2.0 30 9 Product Cut <5.0 241 467 <2.0 <10.0 <20.0 <2.0 6 2 Recycle Strip <5.0 114 128 <2.0 <10.0 <20.0 <2.0 1 <1.0

indicates data missing or illegible when filed

Note that the use of a sodium chloride wash is not economically and results in a solution with too high a sodium content. Without the wash then the lithium chloride stream is contaminated with Na, Ca and K at too high an average concentration. Indeed, it should be appreciated that a very significant reduction in sodium ions is observed, while ions such as Mn and Ca are similar in concentration (which can be purified by known chemical means such as pH adjustment with lithium hydroxide and carbonate and ion exchange to remove impurities). In the comparative example, the concentration sodium ions is 16 g/kg or 0.7 Molal where as in the Li concentration is 2.6 g/kg equivalent to 0.36 Molal. It is shown that the osmotic pressure will be higher under these conditions and that the high sodium content will prevent satisfactory concentration by reverse osmosis. Furthermore there is a significant consumption of salt in the salt wash methodology. In contrast, in the inventive method the amount of sodium in the product cut is 0.46 g/kg 0.02 Molal against the 1.8 g/kg for Li which is 0.25 Molal. Hence the osmotic pressure is almost entirely a function of the Li content and not the sodium content and it will therefore be economically feasible to concentrate the LiCl from 0.5% to approximately 5 wt. % LiCl. Table 14 provides a typical product composition for the comparative method (example 101) and the inventive method (example 102).

TABLE 14 Product B Ba Ca Cd Cu Fe K Li Mg Mn Na Pb Rb S Si Sr Zn Cut mg/kg Example 17 1 299 1 159 2580 6 183 16123 2 10 20 2 4 5 101 Example 102 <1.0 367 <0.5 <0.5 <1.0 149 1800 <5.0 241 467 <2.0 <10.0 <20.0 <2.0 6 2 102

Among other benefits, it should therefore be appreciated that recycling of a lithium rich fraction as described above has numerous benefits, particularly where the resultant lithium solution will be subjected to a downstream reverse osmosis concentration step. Among other things, conventional elution methods that will take advantage of the lithium peak area (and even areas trailing the peak) as illustrated in FIG. 11 will necessarily be also rich in sodium. Therefore, high lithium recovery is associated with high sodium concentrations. Unfortunately, such high sodium concentrations will adversely affect reverse osmosis as sodium substantially contributes to the osmotic pressure. As can be seen from the table above, sodium ions are in six-fold excess over lithium ions using conventional elution. In contrast, when the product (or fractions at least partially overlapping with the product cut) is recycled to the sorbent, the ionic strength is still sufficient to maintain (and even additionally bind) lithium on the sorbent, in large part due to elevated lithium concentration relative to sodium. Viewed from another perspective, ionic strength is gained by an increase in lithium at concomitant decrease of sodium, which favorably affects the product composition upon elution with a suitable eluent low or depleted in sodium. As can also be taken from the table above, the lithium concentration is now approximately four-fold over the sodium concentration. Therefore, partial recycle as presented above allows for an increase in ratio between lithium and undesirable other cations (and especially sodium) while maintaining overall lithium recovery.

The methods described herein are suitable for the recovery of lithium from brines or solutions having low or high lithium concentrations, in addition to brines or solutions that include significant concentrations of other ions, including multivalent ions.

As is understood in the art, not all equipment or apparatuses are shown in the figures. For example, one of skill in the art would recognize that various holding tanks and/or pumps may be employed in the present method.

The singular forms “a”, “an” and “the” include plural referents, unless the context clearly dictates otherwise.

Optional or optionally means that the subsequently described event or circumstances may or may not occur. The description includes instances where the event or circumstance occurs and instances where it does not occur.

Ranges may be expressed herein as from about one particular value, and/or to about another particular value. When such a range is expressed, it is to be understood that another embodiment is from the one particular value and/or to the other particular value, along with all combinations within said range.

Throughout this application, where patents or publications are referenced, the disclosures of these references in their entireties are intended to be incorporated by reference into this application, in order to more fully describe the state of the art to which the invention pertains, except when these reference contradict the statements made herein.

As used herein, recitation of the term about and approximately with respect to a range of values should be interpreted to include both the upper and lower end of the recited range.

Although the present invention has been described in detail, it should be understood that various changes, substitutions, and alterations can be made hereupon without departing from the principle and scope of the invention. Accordingly, the scope of the present invention should be determined by the following claims and their appropriate legal equivalents. 

1-20. (canceled)
 21. A method of extracting lithium from a lithium containing solution, the method comprising: processing a lithium containing solution in a lithium capture step, wherein the lithium capture step includes: contacting the lithium containing solution with a sorbent material to capture lithium; stripping the sorbent material to produce an eluate; recycling at least a portion of the eluate back to the sorbent material, wherein the portion of the eluate comprises the highest concentration of lithium; recovering lithium from the eluate after the recycling step to produce a lithium rich stream; and concentrating the lithium rich stream by processing the lithium rich stream in a reverse osmosis step to produce a concentrated lithium rich stream.
 22. The method of claim 21, wherein the lithium rich stream comprises divalent ions and borate ions.
 23. The method of claim 22, further comprising purifying the lithium rich stream to remove divalent ions and borate ions.
 24. The method of claim 21, wherein the portion of the eluate has a higher lithium to sodium ratio as compared to the lithium containing solution.
 25. The method of claim 21, wherein the reverse osmosis step is a cascade reverse osmosis system.
 26. The method of claim 21, further comprising a purification step for decreasing the concentration of at least one of calcium, magnesium, manganese, or zinc in the lithium rich stream after the lithium capture step, the purification step comprising: contacting the lithium rich stream with a base or a carbonate such that at least a portion of the calcium, magnesium, manganese, or zinc precipitates as a solid carbonate salt; and separating the solid carbonate salt from a purified lithium rich stream, said purified lithium rich stream having a lower concentration of at least one of calcium, magnesium, manganese, or zinc.
 27. The method of claim 21, further comprising a purification step for decreasing the concentration of at least one of calcium, magnesium, manganese, or zinc in the lithium rich stream after the lithium capture step, the purification step comprising: contacting the lithium rich stream with a base and/or a carbonate wherein at least a portion of the calcium, magnesium, manganese, or zinc precipitates as a solid carbonate salt; separating the solid carbonate salt from a purified lithium rich stream; and treating the resultant lithium containing solution with an ion selective media to further remove trace concentrations of divalent ions and boron; wherein the purified lithium rich stream having a lower concentration of at least one of calcium, magnesium, manganese, zinc, or boron.
 28. The method of claim 21, wherein said lithium capture step selectively isolates lithium and substantially allows other cations present in the lithium containing solution not to be co-extracted.
 29. The method of claim 21, wherein the lithium capture step comprises the step of contacting the lithium containing solution with a lithium sorbent material for capturing lithium until the lithium sorbent material is saturated with lithium to produce a saturated lithium sorbent material.
 30. The method of claim 29, the lithium capture step comprises stripping the saturated lithium sorbent material with water to produce the lithium rich stream.
 31. The method of claim 29, wherein the lithium sorbent material is an intercalated lithium sorbent.
 32. The method of claim 29, wherein during the step of contacting the lithium sorbent material and the lithium containing solution, a temperature of the lithium containing solution is maintained above about 70° C.
 33. The method of claim 21, further comprising processing the lithium containing solution in a silica management step to remove silica and to produce a silica-lean lithium solution before supplying the silica-lean lithium solution to the lithium capture step.
 34. A method of extracting lithium from a lithium containing solution, comprising: providing a lithium containing solution including divalent ions and borate ions; processing the lithium containing solution in a silica management step to remove silica from the lithium containing solution and to produce a silica-lean lithium solution; processing the silica-lean lithium solution in a lithium capture step, wherein the lithium capture step includes: contacting the silica-lean lithium solution with a sorbent material to capture lithium; stripping the sorbent material to produce an eluate; and recycling at least a portion of the eluate back to the sorbent, wherein the portion of the eluate comprises the highest concentration of lithium; and recovering lithium from the lithium capture step to produce a lithium rich stream.
 35. The method of claim 34, further comprising purifying the lithium rich stream to remove divalent ions and borate ions; and purifying the concentrated lithium rich stream by removing sodium and potassium ions to produce a concentrated lithium rich solution having reduced sodium and potassium ion concentrations.
 36. The method of claim 35, further comprising further concentration of the concentrated lithium rich stream by solvent extraction.
 37. The method of claim 35, further comprising further concentration of the concentrated lithium rich stream by evaporation.
 38. The method of claim 34, wherein the portion of the eluate has a higher lithium to sodium ratio as compared to the lithium containing solution. 